Emulsion treaters and emulsion treating methods



Dec. 31, 1963 c. o. GLASGOW 25,504

EMULSION TREATERS AND EMULSION TREATING METHODS Original Filed Feb. 16, 1959 4 Sheets-Sheet l 77 BY Q22;

ATTORNE Y Dec. 31, 1963 c. 0. GLASGOW Re. 25,504

EMULSION TREATERS AND EMULSION TREATING METHODS Original Filed Feb. 16, 1959 4 Sheets-Sheet 2 INVENTOR. CLARENCE O. GLASGOW BY Q21 z Kiuz ATTORNEY Dec. 31, 1963 c. o. GLASGOW Re. 25,504

EMULSION TREATERS AND EMULSION TREATING METHODS Original Filed Feb. 16, 1959 4 Sheets-Sheet 3 FUEL INLET +CO0LAN7' WELL STREAM INLET CO0LANT4- WATEQ OUTLET GAS OUTLET INVENT OR.

CL APENCE O. GLASGOW ATTORNEY c. o. GLASGOW Re. 25,504

Dec. 31, 1963 EMULSION TREATERS AND EMULSION TREATING METHODS 4 Sheets-Sheet 4 Original Filed Feb. 16, 1959 INVENTOR. CLARENCE O GLASGOW ATIDRNEY United States Patent 0 25.594 EMULSION TREATERS AND EMULSION TREATING lvlETllGDS Clarence 0. Glasgow, Tulsa, 0kla., assignor to National Tani; Company, Tulsa, Girlie, a corporation of Nevada Original No. 3,899,536, dated Nov. 21, 1961, Ser. No. 73 3,596, Feb. 16, E59. Application for reissue Sept. 6, 1962, Ser. No. 222,769

51 Claims. (Cl. 55-42) Matter enclosed in heavy brackets 1 appears in the original patent hut forms no part of this reissue specification; matter printed in italics indicates the additions made by reissue.

The present invention relates to emulsion treaters and emulsion treating methods. The invention is particularly concerned with processing oil well production in the field in order to separate the production into oil, Water and gas.

Oil well production varies widely in quality, between localities. Sonic black asphaltic base crude oil production in various parts of the WOIlLl has relatively little gaseous phase and its gravity is low, in the order of 25 or 39 API to 9 or 10 API. This production often has a gr at deal of foam. Also the union between the Water and oil is relatively strong, or tight. On start-up, dur ing intermittent treating operation, the low gravity production is diificult to melt from its congealed condition in the treating apparatus, particularly the coalescing section. The foam is difiicult to reduce quickly and etfectively. When a single source of heat is applied to the production to break the tight emulsion, the shin temperature of the heat source must be developed so high that thermal decomposition of the hydrocarbons results in coking of the surface of the heat source. Also, if the production is not passed over the heat source with relatively long residence time, and there is a relatively high skin temperature required, thermal agitation Will not be developed with which to wet the surface of the heat source and prevent vaporization of the mineralcarrying water of the production, leaving scale deposits on the surface of the heat source.

Another problem met in areas producing these black asphaltic base crude emulsions is a dimensional one of the apparatus in which the process is carried out. Local ordinances may prohibit these structures extending as high as a common vertical treating vessel. The lease owner may to cooperate with civic programs to shield unsightly treating apparatus from the public gaze. Also, in remote areas, labor may not be available with whi h to set the vertical structures. Therefore, the pee l ar treating problems of these productions have added lo the problem of solving the treating problems in apparel which is horizontally arranged.

A prirmry object of the prese t invention is to apply a source of heat us to reduce the foam of oil well pro- .on effectively at the b inning of its treating process.

Another olricct is to supp.y heat to oil well production so as to greatly reduce, or eliminate, c king and/or scaling on the surface of a heat source.

Another object is to mechanically manipulate oil well production and apply heat to it at a plurality of locations so as to thoroughly mix the production with any emulsion-breaking chemical that may have been added and raise the temperature of the production to Where it is completely prepared for optimum coalescence of its Water and oil.

Another object is to conserve the gravity of the final clean oil product by condensing all liquefisble compo nents of the gas evolved from the production prior to coalescence of the water and oil while preventing con- Re. Eiifid l Reissuecl Dec. 31,

densation of water vapor from gas above the clean oil back into the clean oil as it is removed from the process.

Another object is to develop a dillcreutul between the pres urcs on surfaces of liquids in die treating prcc ss to move the production liquids through the steps ot the process.

Another object is to provide a structural arrangement vessel compartments in w ich the treating process take?- place, the vessel comparuncnts being in substantin! horizontal alignment.

The present invention contemplates treating a lowgravit", high viscosity, foaming oil well production by y healing the production by dispersion: it in a body ar -r] production which has been heated enough to skin .l"" l'.l'd oi a. sub? :nt l .2 source need not he so high that it will cause ther. c

of hydrocarbons on its surface.

The invention further contcn ed in the body of Ewntcxfij pm. manipulate the production in spre washed therein into thin sheets from lighter hydrocarbon gas will rearny evolve. or brc 'out, in foam reduction and reload and Wlll" c..usc the production to heat more cf? icntly in osity reduction and which will cause he production to min more thoroughly with sny cmulsiombrc king chemical added.

The invention further contemplates the initial heating being followed by a second heating with a source of host hot enough, in a body of the production enough, to set up thermal currents which thoroughly :nitute the body of production in completing the mixing with the chemical and raising it to the temperature where it is completely prepared for optimum coalescence of its water and oil. The production is flowed downwardly over the second source of heat so the final stage of d sing is accomplished in the upper region of the body of production and disturbance from deg: sing is kept to a minimum. The production has been reduced in viscosity by the first heating so the shin temperature of the second heat source need not be high enough to result in scaling and coking in getting the production up to the final treating temperature.

The invention further contcmp from the plur' l st hosting b r c acted through a heat exchanger in u ch 11 cool stream of lluid comic all liquciiable components of the gas cfd the liquids are returned to the production pv irig dot. iwurdly over the llC g ns evolved n oil pro-d combints s19 30. However, 1 heating to the sub passed over the surface of the t ing with any gas evolved neov. the liquids passed from the init sequent heating are heat-excite d with the gas to prevent condensation of any water vapor therefrom into the clean oil.

The invention further contcrnpl-'"tes s g the level of liquids llowecl downwnriil over the nd source of heat and controlling the Withdrawing or toe gas evolved from the liquids of the production heated in developing a differential between the pressure on the surface of liquids heated and the pressure on the clean oil to move clean oil from the process to storage or use, and at any do ibis Working pressure within the safe range of the vescl.

The present invention further contemplates :1 series of duction to within the range which will completely prepare production for optimum coalescence of its water and oil. Also, substantially all of the gas to be evolved at the line] treating temperature will be so evolved in the upper rcrions of compartment 12.

A ten rrtture element 21 is indicated as positioned l" ow the tube of heater l l. Element 21 controls the gasliring heater 14, similar to the control of heater by clan t 6. it is contem late that element 21 will be located in the liquids or": compartment 121 at a position where the control exerted over heater 14 will result in bringing the liquids to within the desired range of tempcrzrture as they leave the bottom of compartment 12 through opening 22.

The final heating afforded by heater 14 is accomplished eT." rally. and with little coking and scaling on the heater tubes. The lowered viscosity provides a rcluti cly high rate of heat transfer from the tubes of heater M to get tem erature at element 7.1 to within the desired range of temperature with the minimum consumption of fuel. The SLFTIICSEiO'il of the skin temperature of heater id to a minimum also rcsults in avoiding the coking and scaling on the surface of the heater M which would take place, at

' :er skin tempe atures.

felting is basically a result of thermal decomposition of hydrocarbons. The lower the temperature to whici the by 'ocarbons are exposed, the less coking will occur. "therefore, the suppressed skin temperature of heater 14 is a basic contribution to this result. Also. however, the thermal currents set up in compartment 12 promote oilwctiinr; of the surface of heater 1d by the agitation. Oilvtztting oi the surface of hCutcr E4 militates against scale.

is basically a result of vaporizing mineral-carrying water in the production. The suppressed skin temperature. of course, reduces the scaling possibili However, the oil-wetting cf the surface of heater 14 reduces the possibility of scale formation. Water has far less tendency to s "'ze on an oil-wctted surface and leave any mineral .cd therein. The thermal agitation in compartment auses oil to continually wipe the heater l4 surface keep it wettcd. The resulting scale reduction follows. 'ihc breaking of the union between the oil and water r :onents of the production, which began in compartm .t El. culminates in the lower regions of compartment The h at from the plurality of sources provided rtmeuts raises the temperature of. the producs the production and thoroughly mixes the crluction with any emulsion-breaking chemical introcd therein. By the time the production has traveled heater i in compartment 12,. l: perof the has been broken away from the oil. the co water at 23 represents, in part, that 'ipitntcd drnvrmardly from comparh water is removed through conduit 24 in water wt mcut 12. This ordwnce wi l the control exerted by a float 25. The K i ssing through opening from run Us been completely prepared for opticoalcsccnce within :1 structure provided in a third truest of vessel 1.

All gaseous components evolved in the first compartmert 3. within the elongated passage of partition ill. and the upper regions of compartment 12, are past-ed out shell It through a conventional mist extractor structure mounted in g head 16. A heat crchanger l; is mounted on the top of as head to. All the gaseous components evolved arc bro s it into heat exchongcr l7 and into int contact with a stream of coolant. This stream of coolant is indi ated coming to heat exchanger 17 n conduit st} and leaving heat exchanger 17 through conduit 19. The coolant provided for heat exchangercondcntcr 17 may be from any cool stream of fluid available. "the well stream of conduit 2 may well have a temperature adequate for this purpose. Of course. any cool streum of water available within the proper temperature range can be used.

6 It is contemplated that all liqucliable comro cnts cf the gaseous stream passing up through head U will fall back through head 16 and onto partition ill. p rtition directly above compartment 12, these cor liquids will join the liquids dropped into compartment l]. through opening 11. The uncondcnsctl p0 tron of the gascs up through head I are removed from cont rr heat exchanger 17 through conduit 2t]. fonduit 15G in1ioduces these gaseous components back into 5 trcatcr. Should there be any liquid car exchanger 17. conduit 29 extends down into cc. L 26 for enough to place the liquids well below the su of the clean oil produced. Holes EllA place the gas l'r conduit 2t} above the clean oil surface in cumpartmr Third compartment 26 is provided between first s ,e-rtmcnt 3 and second compartment 12 within shell l. 'ihc compartment 26 is more specifically defined by purtition a portion of partition it and partition 13. vcl'i l partition 13 extends down from partition i to :1 oint above the bottom of shell 1. to provide the opcnir i.

A conventional hay section is provided nett tion 4 and partition 13 to act as a treating structure for the emulsion passed by up throueh it it opening 22. The hay section 27 illustrated is shown having two sections defined by horizontal imr crlorzrts plates and expanded metal sections. The expanded metal sections and imperforate plates are arranged to provide a serpentine path upward for the emulsion frpsrtment 1" The coalescing function of a is well known. The globules of oil agglomerated in coalescing hay will migrate upward, and the droplets oi \Vtiifil agglomerated by the section will migrate downward to join the collected body of water The result is to collect a body of clean oil in the upper portion of compartment 26 above the buy section from which oil will be removed from vessel 1 by a skimmer 28 through conduit 29.

The three compartments within shell 1 are i'ilustraied in horizontal alignment. Obviously. it is ten ble to f lt vide separate vessels. as compartments. which can be connected by conduits through which to more the tin of the process. Arranged as they are, the thrcc comp merits of vessel 1 have the problem of forcing the clean oil from the collection of oil in the ucpcr portfon or compartment 26. It is difficult to provide a suhicicnl ltcud for this purpose in a horizontal vessel. he present invention provides a substitute for this head force.

The uncondensed gases of conduit 28. from the top of exchanger-condenser 17 are placed on the top of the c oil surface in compartment 26 through driercntial v. 3t}. Conduit 31 is provided to remove this gas from the surface of the clean oil in compartment 26 for any desired manner. it is contemplated that the di: location for the gases of conduit 31 has a p1 sure stantially less than the pressure developed in evolving up through the head 16 and into c Therefore, a modulation of the position of vwlic develop a dillcrentiol of pressure between t e first two compartments and com trnent 26 above the surloce of the clean oil. This diilerential of pressure w ll trov' th: force on the suriace of the liquids in compui lnu'zul' which will remove the liquids from compartment l3, into compartment 26 and out conduit 29.

Differential valve 3t is modulated from the level of liquids in compartment 12. Specifically, float is octuated by the surface of the compartment l2 lie 'rls velop a control force for (lillCICfllllll valve liquid inventory in compartment 12 increases f supply from the conduit above horizontal part float 32 will develop a control pressure for dilml i valve 3i) which will move valve Ell closed. incrcssi g diflercntial pressure between that pressure on the ill} surface of compartment 12 and that pressure on the ci surface of compartment 26. The result is to move liu 'irs from compartment 12 to compartment 2-5 and remove oil through conduit 29.

is. in}

A safety valve 33 is provided in conduit 34 between gas head to and conduit 31. This provision for the release of excess pressure within shell 1 is desirable should the control system malfunction in the modulation of valve Ell or the hay section plug, or clog, with solid matter.

KG. 1 shows to advantage the unique arrangement of compartments within shell 1 to provide a control of the temperature of liquids and gases within compartment 26. Should water vapor be carried from exchanger-condenser 17 through conduit 26, it would be most undesirable to condense this water vapor into the clean oil removed through conduit 29. Therefore, the arrangement illustrated in FEG. l keeps the gas space above the clean oil in compartment 26 warm enough to prevent condensation of water vapor by reason of heat exchange with the liquids of compartment 3 ELIE which travel along parti tion it} directly above compartment 26 enroute to compartment 12.

liG. 2 illustrates more completely the control float 32 has on differential valve 30 which it modulates. Additionally, a possible position for element 21 in compartment 1?. is illustrated. Float 32 is shown as mechanically actuating a mechanicahfiuid pressure transducer 35 to produce a control iluid pressure in conduit 36 which can be placed on a diaphragm of valve 30 to modulate the position of the valve.

Referring now to FIG. 3, a modification of the FIG. 1 structure is illustrated, also embodying the invention. An elevated cross-section of a shell 40 is shown to illustrate a treating vessel with a horizontally extended longitudinal axis.

Oil well production is conducted into shell 40 through conduit 41 and spread, or dispersed, by the perforations of spreader 42. Spreader 42 is mounted in the bottom of compartment 43, from which position it disperses production from conduit 41 upwardly through the liquids in compartment 43.

Heater 44 is mounted above spreader 42 to heat the liquids in compartment 43, along with the production from spreader 42. Battles 45 are mounted above heater 44 to mechanically manipulate the production as the emulsion and gas is heated in its upward passage.

The temperature of the liquids in compartment 43 is controlled by a system which fires heater 44 from the temperature sensed by element 46. The control system responsive to this temperature is similar to that which includes element 6 in PEG. 1.

The complete process of manipulation and heating of the production in compartment 43 is similar to the process carried out in compartment 3 of FIG. 1. Partition 47 defines the left limit of compartment 43 and the right limit is defined by the right end of vessel shell 40. It is contemplated that compartment 43 will remain substantially full of production [water] with which the dispersed production is heated as it travels upwardly through the {water bathlli [tented production. Production is [Surplus water and production are} withdrawn through opening 43 at the top of compartment 43. Thus, the production receives an initial treating by being heated by the production [water] in compartment 43, is mixed to an extent with any added chemical and has its viscosity lowered and is degassed to an extent.

A tray 5G is mounted near the top of vessel 40, defining the top of compartment 43. Tray 50 is mounted at an angle to the horizontal axis of the vessel so that liquids from opening 48 will flow out of compartment 43 and down over tray 50. Step-baffles 51 are placed at intervals atong tray 50, extending at right angles to the liquid low. This arrangement provides a cascading of the liquids which promotes additional degassing and mixing of the liquids. The degassed liquids from tray 5t) are finally dropped downwardly over heater 52.

.cr is mounted in a vessel compartment de fined substantially between horizontal partition 47 and horizontal partition 53. PEG. 4, is a cross-sectional elevation taken along lines 4-4 in l'lG. 3 to iiiustrate that heater 52 is mounted generally at a right angle to the longitudinal axis of vessel 40. This disclosure serves to illustrate the flexibility oi the arrangement between heater 2 and its compartment 54 which provides for adjusting the size of compartment 54, should this be desired. it other considerations permit, this arrangement specifically provides for partitions 47 and S3 to be placed close together, in contrast the HO. 1 arrangement, to form a compartment 54 which is relatively small. At least one result of this arrangement is the possibility of establishing an overall length of vessel 4%) which is materially less than that of vessel 1. In any event, compartment 54 functions generally in the same manner as compartment 12. 01' FIG. 1.

The production from compartment 43 flows downwardly over heater 52 in compartment 54. Additional gas is released in the upper regions of the compartment 54. The firing or" heater 52 is controlled from element .55 in bringing the production up to treating temperature as it passes out opening 56 to the coalescing section. The thermal agitation by heater 52, the mixing of the production and any added chemical, the final evolvement of gas in the upper regions of compartment 54, the avoidance of coking and scaling, the lowered fuel consumption by heater 52 and the final preparation of the production for optimum coalescence all take place in compartment 54 as they do in compartment 12 of FIG. l.

All gaseous components evolved are passed out of shell 40 through mist extractor 57 mounted in head 58. Heat exchanger 59 functions to liquefy a portion of the gas after the fashion of exchanger 1'7 in FIG. 1. The liquid condensed falls into compartment 54 to maintain the gravity of the final clean oil product of the process.

The third compartment 60 is provided between partitions 53 and 61 for the coalescing section. The coalescing section is formed of hay, or excelsior, at 62, as in compartment 26 of FIG. 1. Battles, as indicated, may form a serpentine path upward for the oil, through section 62. The body of clean oil above the section 62 discharges over the upper edge of partition 61 as a weir. In contrast to the FIG. 1 arrangement, compartment 60 is arranged between compartment 54 and the left end of vessel 40, rather than between the two heating compartments in which the heating of the production is staged. This arrangement retains benefits of the up-flow, down-flow stage heating while providing for heater 52 to be inserted in the compartment 54 from the side of vessel shell 40 in making a more compact arrangement.

The clean oil flowing from section 60, over the upper weir edge of partition 61, collects between partition 61 and the left end of the vessel shell 49, in a body 63. Clean oil is drawn from this collection through conduit 64, valved under the control of float 65.

The gas evolved in the compartments of 43 and 54, are passed out of head 58 and exchanger 59 and into conduit 66. Conduit so passes through valve 67, and conduit 66 introduces the evolved gas into the space above the clean oil in the compartment (id. All gas to the left efpartition 53 is removed through conduit 68. Valve 67 is positioned by a control signal developed by the response of iloat 69 to the level of the liquids in compartment 54.

FIG. 4 shows lloat 69 to further advantage, responding to the liquid level in compartment 54 to develop a tluid pressure with control unit 70 for the diaphragm of valve 67. Controlled in this manner, valve 67 restricts conduit 66 enough to maintain suflicient dillerential between the gas pressures on the liquid surfaces of compartments 54 and 60 to overcome the variable restrictions to liquid flow to the coalescing section 69. The liquid level in compartment 54 is an excellent end-point index of all variables of the process which atiect the how of liquids through the vessel 40. These variables may be in the variation in the production of flow through conduit 41, or in resistance to How through coalescing section an. The resistance to flow through coalescing section 6%] may be due either to the flow friction due to temperature variation or the mechanical impediment of solid particles in the section. In any event, all these variables infiuence the liquid level in compartment 54, and, therefore, are automatically applied to positioning of valve 67 in maintaining a dynamic lluid pressure force to move the liquids out of the vessel 40.

From the foregoing it will be seen that this invention is one well adapted to attain all of the ends and objects hercinabove set forth, together with other advantages which are obvious and which are inherent to the appuratus.

it will. be understood that certain features and subcombinations are of utility and may be employed without reference to other features and subcombinations. This is contemplated by and is Eit] Within the scope of the claims.

As many possible embodiments may be made of the invention without departing from the scope thereof, it is to be understood that all matter herein set forth or shown in the accompanying drawings is to be interpreted as illustrative and not in a limiting sense.

The invention having been described, what is claimed l. The method of treating oil W6 1i production including, maintaining a first body of {water} production within a first predetermined range of temperature, with a first source of heat, passing dispersed oil well production up through the body of [water'j heated production to lower the viscosity of the dispersed production to where foam of the dispersed production will be etlectively reduced, passing Ewater of the heated body andIfl heated production and dispersed production along an elongated common path, after first heating. maintaining a second body of the production .vithin a ond predetermined range of temperature will: a se of heat, pc ug the heater] production and o...pci'.scd {water and} pi til it from the eiongat common path down through the sccond body of the pro tion with residence time suificicnt to thoroughly mix the luction by thermal currents created by the second source of heat and to further degas the production and to prep the production for coalescence, passing the production through a zone of coal' cnec to coalesce the oil and migrtc it upward and come-see the water and migrate it dow. ward. and maintaining vapors ev vcd from the body of oil above the coalescence zone in heat transfer relationship with the herded production and dispersed Eliot water and} production in common path to prevent condensation of water vapor directly onto the surface oi the oil.

2. The method of claim 1 including, developing a pressure differential across the zone of coalescence to force the oil out of the coalescence zone.

3. The method of claim 2 inelu eveloping the pressure differential across the zone of coalescence with the level of the second body of the production within the second predetermined range of temperature.

4. The method or claim 3 including, adding an emulsion-breaking chemical to the production prior to [passing E dispr up the production up through the first body of [water] production heated to the first predetermined range of temperature.

5. The method of claim 3 including, removing the hydrocarbon vapors from the degassed production, cooling the hydrocarbon vapors to condense the portion of them which can be stored under substantially ambient temperatures and pressures, and returning the liquids condensed to the second body of production, Within the second predetermined range of temperature.

6. The method of claim 5 in which the cooling of the hydrocarbon vapors is obtained by heat transfer with the oil well production going to the first body of [water] production heated to a first predetermined range of temporature.

7. The method of treating oil troll production including, heating a first body of production {water} to within a first predetermined range of temperature with a first source of heat, dispersing a foamy oil well production upwardly through the first heated body of [waterfi production to lower the viscosity of the dispersed production to where the foam will be eiicctively reduced, passing the dispersed production downwardly over a second source of heat in a second body of production heated to a second predetermined range of temperature and of a size to give a residence time which will enable the thermal currents developed by the second source of heat to roll and mix and degas the production to a substantial degree, controlling the release of gas from the first and second heating to develop a force on the surface of the production h ted to the second predetermined range of temperature to maintain the level of the surface at a preetermined height, passing the production from the second body heated to the second predetermined range of temperature upwardly through a coalescence zone and collecting the oil above the Zone and withdrawing the oil from the process, and maintaining the collected oil and vapor have the collected oil in heat transfer relationship with iiiC dispersed production and [water] production from the first heated body of [Water] production to prevent condensation of water from the vapor into the oil collected and withdrawn.

8. The method of claim 7 including, adding an emulsion-breaking chemical to the production prior to dispersing the production through the first heated body of E} a production.

9. The method of claim 8 including, removing the gas released from the heating of the duper-sad production, coo. g the released from the dispersed production by heat to condense storagcable liquids therefrom, and returning the condensed liquids to the second body of production heated to the second predetermined range of temperature.

it). The method of treating oil well production including, maintaining a first body of [water] production within a first predetermined range of temperature with a first source of heat, controlling the firing rate of the first source of heat to maintain the skin temperature of the first heat source below that at which coking will occur on the surface of the first heat source, {passing}! dispersing oil well production up through the first body of [water] production to lower the viscosity of the dispersed production to where foam of the dispersed production will be eilectivcly reduced, maintaining a second body of the production within a second predetermined range of temperature with a second source of heat, controlling the firing rate of the second source of heat to maintain the skin tempera ture of the second heat source below that at which coking will occur on the surface of the second heat so. i

the rl'isperrcn' production {water} and produc from the first body of production {Quote-r3} down tlirou h the second body of production with rcwidcncc time cient to tl'.o:oug l mix the production by thermal rents created by the second source of heat and to further degus the production and to prepare the production for flowing the broken emulsion through a zone of coalescence to coalesce the oil a d migrate it upward and coalesce the water and migrate it downward, and withdrawing the go. and water and oil separately.

i l. The method of claim 10 including, developing a rential across the zone of coo. essence to force the oil out of the coalescence zone.

12. The method of claim ll including, developing the urc difl'clrcntial across the zone of coalescence with the level of liquids within the second predetermincd range oi temperature.

13. The method of claim 12 including. adding an emulsionbrenlling chemical to the oil well emulsion prior to ilowin g upwardly all of the dispersed production In be 11 trotted through the first body of {water} production within the fife-l pzcdctcrmined range of temperature.

l-l. method of claim l3 including, cooling the vuii'iitlratun gas to condense storageable liquid hydrocarbons and returning the liquids to the emulsion passed downwardly through the second body of production within the second predetermined range of temperature.

15. The method of treating oil well production includin; main ng a first body of lijwater] production within a first predetermined range of temperature with a first source of heat. contrc g the firing rate of the first source oi heat to maintain the skin temperature of the first heat rce below that at which coking will occur on the surn cc of the first heat source, {passing} dispersing oil well produclion up through the first body of [water] production to lower the viscosity of the dispersed production to where loam of the rlixiperzit'tl production will be effectively cod. maintaining a second body of the production ivlllltll a second predetermined range of temperature with a ond source of heat, controlling the firing rate of the second source of heat to maintain the skin temperature of the second heat source below that at which coking will occur on the surface of the second heat source, passing the nursed production [waterE and production from the fi.st body of production [water] down through the second body of production with residence time suflicient to thoroughly mix the production by thermal currents created by the second source of heat and to further degas the production and to prepare the production for coalescence, llowing the brolten emulsion upwardly through a zone (11' coalescence between the first body of {water} pro :1 within the first predetermined range of temperature and the second body of production within the second prod: mined range of temperature to heat exchange with the broltcn emulsion while oil is coalesced and migrated upward and water is coalesced and migrated downward, and withdrawing the gas and water and oil separarely.

iii. The method of claim l5 including, developing a pressure dillcrential across the zone of coalescence to force he oil out of the coalescence zone.

17. The method of claim 16 including, developing the pressure dilicrential across the zone of coalescence with the lCYCl of liquids within the second predetermined range of temperature.

l3. The method of claim 17 including, adding an emulsion-breaking chemical to the oil well emulsion prior to flowing upwardly all of the production to be treated through the first body of [watcrl production within the first predetermined range of temperature.

l9. The method of claim 28 including, cooling the withdrawn gas to condense storageable liquid hydrocarbons and returning the liquid to the emulsion passed downwardly through the second body of production within the second predetermined range of temperature.

Ill. Apparatus for the treatment of oil well production first source of heat for the h rmlmx-i u, means for rcgulat ot heat to rise the temperature of the 'i r urrcrl ElnElSlCLl] up through the first body pcrsc'rl probe etlcctively reduced, :1 second chambc into which production ljwalcr} from the first body of ijwutsr "TEJLK'H'OH in the first chamber and the dispersed in the second chamber passed downwardly over the second source of heat. means for regulating the second source of heat to produce thermal currents in the production to further degas the production and to prepare the production for coalescence, a third chamber to receive the production and coalesce the oil and migrate it upward and coal:scc the water and migrate it down i ll ward, and a conduit between the first and second chamber; in heat exchange relationship with the third chamber so the heat of the dis, rs'ed m lion EIwutcrIE and production from the first number will prevent condensation of any water vapor above the coalesced oil into the oil.

21. The apparatus of claim 26 including, means responsive to the level or" production in the second chamber controlling the release of gas from the chambers to develop a diii'erential pressure across the third chamber to force tie oil from the third chamber.

1116 apparatus of claim 20 including, means for w a predetermined amount of emulsion-breaking l to the (lilrprrs'ctl production prior to the dispersed production being received in the first chamber.

7 The apparatus of claim ll including, a condenser ing the hydrocarbon vapors from the degassed prom to condense that part of them which can be l un;l:r substantially ambient temperatures and ircs, and means for returning the condensed liquids 1.11: second chamber.

ug'iparatus of claim 23 including, means for so; plying the oil well production to the first chamber to the condenser as a heat exchange medium with which to nae the hydrocarbon vapors.

fi nratus for treating oil well production including, a first source ol heat, a first body of Ewater] prodnrfion heated to within a first predetermined range of temperature by the first source of heat, means for disnur ing a foamy oil well production upwardly through the heated first body of production [water] to lower the vis- .y oi the tits-parsed production until the foam is eflecy reduced, at second source of heat, means for passthe dcioamed production downwardly over the second source of heat and maintaining the production heated in a second body of a size to give a residence time which will enable the thermal currents developed to roll and mi); and further dc as the production to a substantial means to control the release of gas from the and second heating to develop a force on the surface of the production passed downwardly over the second source of heat which will maintain the level at a predctern'iincd height, means defining a coalescence zone, means passing the production from the second source of heat upwardly through the coalescence zone to collect oil at the top of the zone and withdraw the oil from the process, and means arranging the defoamcd production from the first heating in heat exchange relationship with the top ol the coalescence zone to prevent condensation ol water from the vapor at the top of the zone into the coalesced oil.

26. The apparatus of claim 25 including, means for adding a predetermined amount of emulsion-breaking chemical to the production prior to dispersing the proci on through the first body of heated [water] pro- (Indian.

27. The apparatus of claim 25 including, a condenser arranged to cool the gas released from the production by the heating and condense storageable liquids, therem. and means for returning the liquid to the defoamed production wnich was passed downwardly over the second of heat.

. Apparatus for the treatment of oil well production including, a first chamber into which the production is received, a first body of [water] production in the first hamber, a t source of heat for the first body of crfg'l pr: czion, means regulating the first source of t to raise the temperature of the production dispersed E, i used} up through the first body of {water} production to lower the viscosity of the dispersed production to where foam of the dispersal production will be effectively reduced while not elevating the skin temperature of the first heat source so high as to produce coking on the surface of the first heat source, a second chamber into which {water} tr-inflation from the first body of production Ewatcrj in the first chamber and the dispersed produetion is received, a second source of. heat for the production in the second chamber passed downwardly over the second source of heat, means regulating the second source of heat to produce thermal currents in the production to further degas the production and to prepare the production for coalescence while not elevating the skin temperature of the second heat source so high as to produce coking on the surface of the second heat source, a third chamber receiving the production from the second chamber to coalesce the oil and migrate it upward and coalesce the water and migrate it downward, and means for withdrawing the gas and water and oil separately.

29. The apparatus of claim 28 including, means with which a pressure differential is developed between the second and third chambers to force the oil out of the third chamber.

30. The apparatus of claim 29 in which, the means developing the pressure differential is directly responsive to the level of liquids of the second chamber.

31. The apparatus of claim 28 including, a condenser receiving the gas evolved from the first and second cham bers to condense storageable liquid hydrocarbons therefrom and return those liquids to the second chamber.

32. The apparatus of claim 28 including, a means for adding a predetermined amount of emulsion-breaking chemical to the oil well emulsion prior to flowing upwardly all the products to be treated through the first chamber.

33. Apparatus for the treatment of oil Well production including, a first chamber into which the production is received, a first body of [water] production in the first chamber, a first source of heat for the first body or Lwaterj production, means regulating the first source of heat to raise the temperature of the production dispersed {passed} up through the first body of [water] production to lower the viscosity of the dispersed production to where foam of the dispersed production will be effectively reduced while not elevating the skin temperature of the first heat source so high as to produce coking on the surface of the first heat source, a second chamber into which [water] production from the first body of [water] in the first chamber and the dispersed production is received, a second source of heat for the production in the second chamber passed downwardly over the second source of heat, means regulating the second source of heat to produce thermal currents in the production to further dcgas the production and to prepare the production for coalescence while not elevating the skin temperature of the second heat source so high as to produce coking on the surface of the second heat source, a third chamber in the unified vessel located between the first and second chambers and in heat exchange relation to them while oil is coalesced and migrated upward and water is coalesced and migrated downward, and conduits connected to the second and third chambers through which gas and oil and water are separately removed.

34. The apparatus or" claim 33 including, means for developing a pressure diilcrentisl between the second chamber and the third chamber to force oil from the third chamber in its conduit.

35. The apparatus of claim 34 in which the means developing the pressure differential responds to the level of the liquids in the second heating zone.

36. The apparatus of claim 34 including, means for adding a predetermined quantity of emulsion-breaking chemical to the oil veil emulsion prior to flowing all of the products to be treated through the first chamber.

37. The apparatus of claim 35 including, a heat exchanger for cooling the gas of the process sutliciently to condense storageable liquid hydrocarbons from the gas and returning the liquids to the emulsion passed to the second chamber,

38. A horizontal treater for oil well emulsion including, a first compartment in the treatcr shell, a first firc tube in the first compartment controlled to raise the temperature of emulsion flowing upwardly over the firetube to reduce the viscosity of the emulsion and evolve hydrocarbon and water vapors, a second compartment in the treater shell, a second firctuhe in the second coin partmcnt controlled to further raise the temperature of the emulsion flowed downwardly over the firctube from the first compartment until the emulsion film is broltcn as Water is removed downwardly at a rate which militates against substantially heating the water further, a third compartment in the trcater shell into which the oil and broken emulsion of the second compartment is flowed for coalescence of the oil in its top and water in its bottom, a condenser receiving the evolved vapors from the first and second compartments to condense the SlOiGSC able .iquid hydrocarbons from the evolved vapors, and return the liquid to the second chamber, conduit for removing any uncondensed vapor and liquid carryover from the condenser and placing the vapor in the third compartment above the oil surface and the llqllld in the third compartment below the oil surface, and conduits connected to the second and third compartments for withdrawing the gas and water and oil separately.

39. The treatcr of claim 38 including, a coalescing structure in the third compartment, a valve in the conduit between the condenser and the third compartment, and a level responsive means in the second compartment detecting the liquid level controlling the valve to develop a pressure differential between the second and third compartrnents which will force the emulsion from the second compartment and the oil from the third compartment.

40. The method of treating oil well production including,

heating a first body of production with a first source ofheat,

introducing an oil well production through the first heated body of production to lower the viscosity of the introduced production,

passing the introduced production along a flow path in a relatively thin sheet,

passing the introduced production over a second source of heat in a second body of production,

passing the substantially degassed production from the second body of production upwardly through a coalescence zone,

collecting the oil above the zone,

and witlidrmring the oil from the process.

4]. Apparatus for the treatment of oil well production, including,

a first chamber into which the production is received,

a first body of production in the first chamber,

a ix; source ol 1: at for the fit-rt luriy oi r 'olur-im means; for introducing an oil well production through the first limited body of production to lower the vis- (ovity of the introduced production,

an elongated passage connected to the first chamber which conducts the introduced production from the first chamber in relatively tliin Sllt'tl,

a second chamber connected to the elongated puss-ago into which production from the first body of production in the first chamber and the introduced production is reccirt'd,

a second SOi/I'Ct of lieut for the production received in tlse second chamber,

(1 third chamber connected to tlic second clzttml cr (Hill containing a coolest-lug structure which receives the production and coolesces' the oil into (1 lmdy (lbOl'L tltc structure and the lratcr into a body below the structure,

and means for separate removal of oil and writer from the tliird Cllti'lllllfl'.

42. The method of treating oil well production including,

heating: a first body of production with a first source of heat,

towing and dispersing the oil Well production upwardly through the first heated body of production to lower the viscosity of the dispersed production,

passing the dispersed production along a horizontal flow path in a relatively thin sheet,

passing the dispersed production downwardly over a second source of heat in a second body of production,

passing the substantially degassed production from the second body of production upwardly through a coalescence zone,

withdrawing water from below the coalescence zone,

and witiulrauine oil from above the coalescence zone.

43. Apparatus for the treatment of oil Well production including,

a first chamber into which the production is received,

a first body of production in the first chamber,

a first source of heat for the first body of production,

means for dispersituy an oil well production through the first heated body of production to lower the viscosity of the dispersed production and flowing the dispersed production upwardly over the first source of heat,

an elongated passage connected to the top of the first chamber which conducts the dispersed production from the first chamber in a relatively thin sheet,

a second chamber connected to the elongated passage into which production from the first body of production in the first chamber and the dispersed production is received,

a second source of heat mounted in the second chamber and arranged to have the dispersed production flowed downwardly the/cover,

a third chamber connected to the second chamber to receive the production from the second chamber,

a coalescing structure in the third chamber arranged to have the production flowed upwardly therethrough to coalesce the oil and collect it above the structure and coalesce the water and collect it below the structure,

and means for separately withdrawing the oil and water from the third chamber.

44. The method of claim 42 including, developing a pressure diflerential across the zone of coalescence to force oil out of the coalescence zone.

45. The apparatus of claim 43 including, means with which a pressure difierential is developed between the second and third chambers to force the oil out of the third chamber.

46. The method of claim 44 including, developing the pressure differential across the zone of coalescence with the level of the second body of the production.

47. The apparatus of claim 45 in which, the means developing the pressure diflerential is directly responsive to the level of production liquids in the second chamber.

43. The method of claim 42 including, cooling the gas evolved from the production to condense storageable liquid hydrocarbons and combining the liquids with the oil withdrawn.

49. The apparatus of claim 43 including, a condenser receiving gas evolved from the production to condense storageable liquid hydrocarbons therefrom and return those liquids to the oil withdrawn.

50. The method of claim 42 including, adding an emulsion-breahing chemical to the production prior to flowing upwardly all of the dispersed production to be treated through the first body of production.

51. The apparatus of claim 43 including, a means for adding a predetermined amount of emulsion-breakiug chemical to the production prior to flowing upwardly all the dispersed production to be treated through the first body of production.

References Cited in the file of this patent or the original patent UNITED STATES PATENTS 2,598,988 Glasgow June 3, 1952 2,691,903 Erwin July 1, 1952 2,601,904 Erwin July 1, 1952 2,664,170 Walker et a1. Dec. 29, 1953 2,713,919 Walker et al July 26, 1955 2,751,998 Glasgow June 26, 1956 

